CN108530251A - Device and method for gaseous feed stream of the film infiltration processing comprising methane and carbon dioxide - Google Patents

Device and method for gaseous feed stream of the film infiltration processing comprising methane and carbon dioxide Download PDF

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Publication number
CN108530251A
CN108530251A CN201810170651.3A CN201810170651A CN108530251A CN 108530251 A CN108530251 A CN 108530251A CN 201810170651 A CN201810170651 A CN 201810170651A CN 108530251 A CN108530251 A CN 108530251A
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China
Prior art keywords
rich
methane
retention
gas
feed stream
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CN201810170651.3A
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Chinese (zh)
Inventor
G·普林斯
N·帕热
G·齐克
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LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
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LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
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Publication of CN108530251A publication Critical patent/CN108530251A/en
Pending legal-status Critical Current

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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/22—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by diffusion
    • B01D53/225—Multiple stage diffusion
    • B01D53/226—Multiple stage diffusion in serial connexion
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C7/00—Purification; Separation; Use of additives
    • C07C7/005—Processes comprising at least two steps in series
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/22—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by diffusion
    • B01D53/225—Multiple stage diffusion
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/22—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by diffusion
    • B01D53/228—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by diffusion characterised by specific membranes
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C7/00—Purification; Separation; Use of additives
    • C07C7/144—Purification; Separation; Use of additives using membranes, e.g. selective permeation
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
    • C10L3/06—Natural gas; Synthetic natural gas obtained by processes not covered by C10G, C10K3/02 or C10K3/04
    • C10L3/10—Working-up natural gas or synthetic natural gas
    • C10L3/101—Removal of contaminants
    • C10L3/102—Removal of contaminants of acid contaminants
    • C10L3/104—Carbon dioxide
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2256/00—Main component in the product gas stream after treatment
    • B01D2256/24—Hydrocarbons
    • B01D2256/245—Methane
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/50—Carbon oxides
    • B01D2257/504—Carbon dioxide
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2258/00—Sources of waste gases
    • B01D2258/05—Biogas
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
    • C10L2290/46—Compressors or pumps
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
    • C10L2290/00—Fuel preparation or upgrading, processes or apparatus therefore, comprising specific process steps or apparatus units
    • C10L2290/54—Specific separation steps for separating fractions, components or impurities during preparation or upgrading of a fuel
    • C10L2290/548—Membrane- or permeation-treatment for separating fractions, components or impurities during preparation or upgrading of a fuel
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
    • Y02C20/00—Capture or disposal of greenhouse gases
    • Y02C20/40—Capture or disposal of greenhouse gases of CO2
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E50/00—Technologies for the production of fuel of non-fossil origin
    • Y02E50/30—Fuel from waste, e.g. synthetic alcohol or diesel

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  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Engineering & Computer Science (AREA)
  • Organic Chemistry (AREA)
  • General Chemical & Material Sciences (AREA)
  • Analytical Chemistry (AREA)
  • Water Supply & Treatment (AREA)
  • Separation Using Semi-Permeable Membranes (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)

Abstract

Equipment the present invention relates to the gaseous feed stream (6) of methane and carbon dioxide is included at least for film infiltration processing to generate the gaseous stream (12) rich in methane, including：First film separation unit (1), it can receive gaseous feed stream and generate the first rich carbonated retention (7) for being rich in methane through object (4) and first, second film separation unit (2), it can receive the first retention (7) and generate the second rich carbonated retention (8) for being rich in methane through object (5) and second, gas gas injector (11), it can penetrate the pressure of object (4) by first and improve to 26 bars, more preferable 34 bars of pressure, and third film separation unit (3), it can receive the first transmission object (4) compressed in injector and generate retention (9) and third of the third rich in methane penetrates object (10) rich in CO2.

Description

For film infiltration processing comprising methane and carbon dioxide gaseous feed stream equipment and Method
At least gaseous stream containing methane and carbon dioxide being handled to generate richness for film infiltration the present invention relates to a kind of The device and method of gaseous stream containing methane.
More particularly it relates to the purifying of biogas, it is therefore an objective to which production meets the specification of injection natural gas network Biological methane.
Biogas is the gas that organic matter decomposes (anaerobic fermentation) generation during (also referred to as methanation) in the presence of anaerobic Body.This may be a kind of natural decomposition-therefore can observed by marsh or city refuse landfill-but the production of biogas Life is also likely to be by the waste in special purpose reactor (being known as methanation device (methanizer) or boiling vessel (digester)) Methanation caused by.
Since its main component-methane and carbon dioxide-biogas is a kind of potential greenhouse gases；Meanwhile in fossil Under the increasingly rare background of the energy, it is also a kind of important sources of regenerative resource.
Biogas mainly contains methane (CH4) and carbon dioxide (CO2), and ratio depends on the mode obtained and changes, But also water, nitrogen, hydrogen sulfide, oxygen and other micro organic compounds containing smaller ratio.
The ratio of organic substance depending on decomposition and technology used, each component is different；However, biogas is flat based on dry gas Include 30% to 75% methane, 15% to 60% CO2,0% to 15% nitrogen, 0% to 5% oxygen and milligram ammonia Close object.
Value is obtained by biogas in various ways.It can be processed near Workplace after slight processing and The mixture (cogeneration of heat and power (cogneration)) of heat, electric power or both is provided；High carbon dioxide content reduces its heat Value, improves compression and transportation cost, and limits the economic advantages for processing it to use nearby.
More thorough biogas purifying allows that biogas is more widely used；More specifically, the thorough purifying production of biogas It has given birth to and has been purified to natural gas specification and the biogas of the substitute that can be used as the gas；Thus the biogas purified is " biological first Alkane ".Therefore, biological methane utilizes the renewable part supplemental natural gas resource generated in region；It can be used for coming with fossil The identical purposes of natural gas in source.It can supply natural gas network, group refueling station, and can also liquefy and with liquid Change the storage of the forms such as natural gas (LNG).
The mode being worth by biological methane is determined according to local circumstance：Local energy resources demand is fired as biological methane The option for expecting processing, the network especially for distributing or transporting natural gas nearby exist.In the difference of a regional work Synergistic effect is established between network operator (peasant, manufacturer, public body), the production of biological methane contributes to each department in the energy Aspect obtains the self-sufficient of bigger.
Many steps must be carried out between collecting biogas and producing biological methane (can compress or liquefied finished product) Suddenly.
More particularly, before purpose is to detach processing of the carbon dioxide to generate the methane stream of purifying, it is necessary to many Step.The first step is to compress the biogas of production and transportation at atmosheric pressure；The compression can be -normally-to pass through lubrication Helical-lobe compressor obtains.Subsequent step is intended to isolate the corrosive component of biogas, these components are hydrogen sulfide and volatilization Property organic compound (VOC).Technology used is typically pressure-variable adsorption (PSA) and captures on the activated carbon.Following step is Carbon dioxide is detached, to finally subsequently provide methane using required purity with it.
Carbon dioxide is typically found in the pollutant in natural gas, it is often necessary to isolate it by natural gas.For this purpose, Various technologies are used depending on each situation：In these techniques, membrane technology is especially effective when CO2 contents are high；Therefore it for It detaches in biogas, more particularly the CO2 present in landfill gas is especially effective.
Many steps must be completed between biogas and biological methane production, biological methane is can to compress or liquid collecting The final products of change.
More particularly, before processing intent is to detach methane stream of the carbon dioxide to generate purifying, many steps are needed. The first step is to compress the biogas of production and transportation at atmosheric pressure；This compression can with-usually pass through lubricate screw compression Machine obtains.Subsequent step is intended to the biogas of exfoliation corrosion component, these components are hydrogen sulfide and volatile organic compound Object (VOC).Used technology is typically pressure-variable adsorption (PSA) and captures on the activated carbon.Following step is separation two Carbonoxide, finally subsequently to provide methane using required purity to provide.
Carbon dioxide is typically found in the pollutant in natural gas, and usually it must be stripped.It adopts as the case may be With various technologies：In these techniques, membrane technology is especially effective when CO2 contents are high；Therefore it is for detaching biogas, more CO2 especially in landfill gas is especially effective.
Either use one or more mem stages, the gas separation membrane method for purified gases allow for it is low at This production has the gas of required quality, while minimizing the loss of its value gas to be improved.Therefore, pure in biogas In the case of change, the separation carried out is mainly CH4/CO2 separation, and it is super containing (depending on its purposes) to allow for production 85% CH4, the gas of preferably greater than 95% CH4, the gas of more preferably above 97.5% CH4 are crossed, while making residue gas The loss of CH4 and purifying cost minimization, the electricity of purifying cost signal portion and the device of the gas for compressive films upstream in body Power consumption is related.
A kind of known solution is related to using three stage film systems (Fig. 1), wherein the first stage through object 4 the It is subjected to second of separation in three mem stages, is then mixed into being recycled through object 5 for second stage.Three stage system is no longer Penetrating for compression first stage uses under object, and the residual product through object and phase III of second stage is recycled to film The entrance of system.Relative to two benches membranous system, which improves methane production.
One key parameter of three stages construction is that the section of the first rank penetrates the pressure of object, this is the entrance pressure of phase III Power.Therefore, two conflicting targets are mutually contradictory：
1. pressure minimum must be made to improve the efficiency of first stage；
2. must make pressure maximum needs membrane module number to be mounted to improve the efficiency of phase III or reduce.
In order to confirm the effect through object pressure of first stage, Fig. 2 show CH4 yields and standardize specific cost with The variation through object pressure of first stage.
Fig. 2 shows if retaining every other parameter, the minimum bigger of pressure.
However, in order to be benefited in the maximal efficiency by the phase III, it is desirable to increase the entrance pressure in the stage, this can lead to Mechanical compressor is crossed to carry out.
A solution according to the present invention is the gaseous state including at least methane and carbon dioxide for film infiltration processing Equipment of the feeding flow 6 to generate the gaseous stream 12 rich in methane, the equipment include：
- the first film separation unit 1, can receive gaseous feed stream and generation first is rich carbonated through object 4 and first be rich in methane retention 7,
- the second film separation unit 2 can receive the first retention 7 and generate the second rich carbonated transmission Object 5 and second is rich in the retention 8 of methane,
Gas-gas injector 11, the pressure that object 4 can be penetrated first are improved to 2-6 bars, more preferable 3-4 bars Pressure, and
Third film separation unit 3 can receive compressed in injector first through object 4 and generate third and be rich in The retention 9 and third of methane penetrate object 10 rich in CO2.
In appropriate circumstances, equipment according to the present invention can have one or more following characteristics：The equipment Include the device for the part B of gaseous feed stream to be delivered to gas-gas injector, and gas-gas injector is Using the part B of gaseous feed stream as the gas-gas injector of power gas (motive gas),
The equipment includes compressor, can will be carried in the pressure of the gaseous feed stream of the first film separation unit upstream Up to more than 8 bars, more preferably larger than 13 bars of pressure,
The equipment includes the 4th film separation unit, can receive third through object and generate the 4th rich in methane Retention and the 4th rich in CO2 penetrate object,
The equipment includes penetrating the device of object for swimming joint recycling third retention and second on the compressor,
The equipment includes penetrating the device of object for swimming joint the 4th retention of recycling and second on the compressor,
The equipment includes the device for penetrating object in device external discharge third,
The equipment includes the device for the 4th retention to be discharged in device external,
The having the same selective or different selectivity of the films of-three film separation units.
Another theme of the present invention is a kind of gaseous feed stream 6 that film permeates processing including at least methane and carbon dioxide Method to generate the gaseous stream 12 rich in methane, uses equipment as defined herein and includes：
A) UF membrane gaseous feed stream is rich carbonated through object 4 to generate first in the first film separation unit 1 The first step for the retention 7 for being rich in methane with first,
B) the first retention of UF membrane 7 is rich carbonated through object 5 to generate second in the second film separation unit 2 The second step for the retention 8 for being rich in methane with second,
C) the step of being compressed to 2-6 bars of pressure through object 4 by first by gas-gas injector 11,
D) first compressed in UF membrane injector 11 in third film separation unit 3 is rich in through object 4 with generating third The retention 9 and third of methane are rich in the third step through object 10 of CO2.
In appropriate circumstances, there can be following one or more following characteristics according to the method for the present invention：
Gas-gas injector 11 is using the part B of gaseous feed stream as power gas.
In the upstream of the first film separation unit 1, gaseous feed stream 6 is compressed to more than 8 bars, more preferably larger than 13 bars Pressure.
The method includes UF membrane thirds to be rich in CO2 through object to generate the 4th retention and the 4th rich in methane The four steps through object.
Third retention 9 and second is swum to joint recycling on the compressor through object 5.
4th retention and second are swum into joint recycling through object on the compressor.
For the present invention, gaseous feed stream be preferably derived from for example digester(-tor), installation for fermenting, waste disposal facilities or The biogas of WTP (WTP=sewage treatment plants).
Apparatus and method according to the invention is improved to 2-6 bars of pressure, in other words by penetrating the pressure of object by first It says, by making pressure is " mild " to improve so that lower the film surface product installed in the phase III, and therefore keeping constant production Capital cost is reduced while amount, or improves the efficiency of apparatus/method according to the present invention.
Since the power gas that gas-gas injector uses is not deposited from the gaseous feed stream of first stage In pollution risk.In addition, injector has the advantages that be free of moving parts.
Description of the drawings
Fig. 1 shows that a kind of known solution is related to using three stage film systems.
Fig. 2 shows CH4 yields and standardizes variation through object pressure of the specific cost with the first stage.
Fig. 3 shows that being handled for film infiltration for a solution according to the present invention includes at least methane and titanium dioxide Equipment of the gaseous feed stream 6 of carbon to generate the gaseous stream 12 rich in methane.

Claims (15)

1. a kind of including at least the gaseous feed stream (6) of methane and carbon dioxide to generate rich in methane for film infiltration processing The equipment of gaseous stream (12), including：
- the first film separation unit (1), can receive gaseous feed stream and generation first is rich carbonated through object (4) The retention (7) for being rich in methane with first,
- the second film separation unit (2), can receive the first retention (7) and generation second is rich carbonated through object (5) and second be rich in methane retention (8),
Gas-gas injector (11), the pressure that object (4) can be penetrated first are improved to 2-6 bars, more preferable 3-4 bars Pressure, and
Third film separation unit (3) can receive compressed in injector first through object (4) and generate third richness Retention (9) and third containing methane penetrate object (10) rich in CO2.
2. equipment according to claim 1, it is characterised in that the equipment include for by the part B of gaseous feed stream by first Film separation unit is delivered to the device of gas-gas injector, and gas ejector is made using the part B of gaseous feed stream For the injector of power gas.
3. according to the equipment of claims 1 or 2, it is characterised in that the equipment includes compressor, and the compressor can be The pressure of gaseous feed stream is risen above 8 bars by one film separation unit upstream, more preferably greater than 13 bars of pressure.
4. equipment according to claim 3, it is characterised in that the equipment includes the 4th film separation unit, the 4th UF membrane Unit can receive third and penetrate object rich in CO2 through the retention of object and generation the 4th rich in methane and the 4th.
5. equipment according to claim 3, it is characterised in that the equipment includes for trip joint recycling the on the compressor The device of three retentions and the second transmission object.
6. equipment according to claim 4, it is characterised in that the equipment includes for trip joint recycling the on the compressor The device of four retentions and the second transmission object.
7. equipment according to claim 3, it is characterised in that the equipment includes for penetrating object in device external discharge third Device.
8. equipment according to claim 4, it is characterised in that the equipment includes for the 4th retention to be discharged in device external Device.
9. equipment as claimed in one of claims 1-8, it is characterised in that the film of three film separation units has identical Selectivity or different selectivity.
10. film infiltration processing is including at least the gaseous feed stream (6) of methane and carbon dioxide to generate the gaseous feed rich in methane The method of (12) is flowed, the method is using the equipment as defined in any one of claim 1-9 and includes the following steps：
A) UF membrane gaseous feed stream is rich carbonated through object (4) to generate first in the first film separation unit (1) The first step for the retention (7) for being rich in methane with first,
B) the first retention of UF membrane (7) is rich carbonated through object to generate second in the second film separation unit (2) (5) and second rich in methane retention (8) second step,
C) the step of being compressed to 2-6 bars of pressure through object (4) by first by gas-gas injector (11),
D) it is rich to generate third through object (4) for first compressed in UF membrane injector (11) in third film separation unit (3) The third step through object (10) of retention (9) and third containing methane rich in CO2.
11. method according to claim 10, it is characterised in that the gas-gas injector (11) is using gaseous feed stream Part B is as power gas.
12. according to the method for claim 10 or 11, it is characterised in that in the upstream of the first film separation unit by gaseous feed stream (6) it is compressed to more than 8 bars, more preferably greater than 13 bars of pressure.
13. method according to claim 12, it is characterised in that the method includes UF membrane third penetrants to generate the 4th Retention and the 4th rich in methane are rich in the four steps through object of CO2.
14. method according to claim 12, it is characterised in that third retention (9) and second penetrates object (5) in compressor Upstream joint recycling.
15. method according to claim 13, it is characterised in that the 4th retention and second joins through object in the upstream of compressor Close recycling.
CN201810170651.3A 2017-03-02 2018-03-01 Device and method for gaseous feed stream of the film infiltration processing comprising methane and carbon dioxide Pending CN108530251A (en)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
FR1751688A FR3063437B1 (en) 2017-03-02 2017-03-02 APPARATUS AND METHOD FOR MEMBRANE PERMEATION TREATMENT OF A GAS SUPPLY FLOW COMPRISING METHANE AND CARBON DIOXIDE
FR1751688 2017-03-02

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EP (1) EP3369473A1 (en)
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Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN111321022A (en) * 2018-12-14 2020-06-23 乔治洛德方法研究和开发液化空气有限公司 Apparatus and method for osmotically treating a gas stream through a membrane with an adjusted suction pressure of a second permeate

Families Citing this family (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US11155760B2 (en) * 2019-04-30 2021-10-26 Honeywell International Inc. Process for natural gas production
FR3097450B1 (en) * 2019-06-20 2021-11-19 Air Liquide Treatment of a methane stream comprising VOCs and carbon dioxide by combining an adsorption unit and a membrane separation unit
FR3097774B1 (en) * 2019-06-26 2021-05-28 Air Liquide Plant for the treatment of a flow of methane and carbon dioxide by means of a vane compressor and a membrane separation unit
FR3112085B1 (en) * 2020-07-03 2023-11-17 Air Liquide Use of a flow of carbon dioxide from the membrane separation of biogas to inert a means of storage of at least one agricultural commodity
FR3120803A1 (en) * 2021-03-22 2022-09-23 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Plant for treatment by membrane permeation of a biogas stream with a two-module membrane separation unit
US11980846B1 (en) 2023-08-18 2024-05-14 Unconventional Gas Solutions, LLC System and method for producing renewable natural gas from biogas

Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4386944A (en) * 1980-07-24 1983-06-07 General Electric Company System and process for increasing the combustible component content of a gaseous mixture
EP2196252A1 (en) * 2008-12-11 2010-06-16 General Electric Company System and method for CO2 capture with membrane and ejector
EP2735355A1 (en) * 2012-11-27 2014-05-28 Technische Universität Wien Permeator system for separating gas mixtures

Family Cites Families (14)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4339917A (en) * 1979-06-13 1982-07-20 The Garrett Corporation Fuel delivery system and method
JPS63248418A (en) * 1987-04-02 1988-10-14 Ube Ind Ltd Separation of gaseous mixture
FR2724327B1 (en) * 1994-09-12 1996-10-25 Air Liquide METHOD FOR CASCADE MEMBRANE SEPARATION OF MEMBRANES OF DIFFERENT SELECTIVITY
US6168649B1 (en) * 1998-12-09 2001-01-02 Mg Generon, Inc. Membrane for separation of xenon from oxygen and nitrogen and method of using same
US6630011B1 (en) * 2002-09-17 2003-10-07 Membrane Technology And Research, Inc. Nitrogen removal from natural gas using two types of membranes
ITMI20040648A1 (en) * 2004-03-31 2004-06-30 Saipem Spa PROCEDURE FOR THE TREATMENT OF FLUIDS COMING FROM SUBMARINE OIL FIELDS
US9630141B2 (en) * 2009-02-20 2017-04-25 Cameron Solutions, Inc. Membrane filter element with multiple fiber types
US9017451B2 (en) * 2012-03-16 2015-04-28 Membrane Technology And Research, Inc. Membrane-based gas separation process using ejector-driven gas recycle
KR101559201B1 (en) * 2013-02-19 2015-10-12 주식회사 엘지화학 Membrane sepreation apparatus
ES2583903T3 (en) * 2013-07-30 2016-09-22 Haldor Topso¿E A/S Procedure to produce high purity CO by purification with CO membrane produced by SOEC
AT515137B1 (en) * 2013-12-02 2016-01-15 Johann Gruber-Schmidt Process for the separation, purification and concentration of gas mixtures
KR101535026B1 (en) * 2014-06-12 2015-07-07 현대자동차주식회사 Humidifier for Fuel Cell System
EA034642B1 (en) * 2014-12-29 2020-03-02 Эвоник Фибрес Гмбх Process for separation of gases with reduced maintenance costs
US20190358582A1 (en) * 2018-05-23 2019-11-28 James Khreibani System and process for separating gas components using membrane filtration technology

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4386944A (en) * 1980-07-24 1983-06-07 General Electric Company System and process for increasing the combustible component content of a gaseous mixture
EP2196252A1 (en) * 2008-12-11 2010-06-16 General Electric Company System and method for CO2 capture with membrane and ejector
EP2735355A1 (en) * 2012-11-27 2014-05-28 Technische Universität Wien Permeator system for separating gas mixtures

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN111321022A (en) * 2018-12-14 2020-06-23 乔治洛德方法研究和开发液化空气有限公司 Apparatus and method for osmotically treating a gas stream through a membrane with an adjusted suction pressure of a second permeate

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